US4187175A - Treatment facility with backwash control system - Google Patents

Treatment facility with backwash control system Download PDF

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Publication number
US4187175A
US4187175A US05/918,593 US91859378A US4187175A US 4187175 A US4187175 A US 4187175A US 91859378 A US91859378 A US 91859378A US 4187175 A US4187175 A US 4187175A
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United States
Prior art keywords
backwash
flow rate
rate
backwash liquid
liquid flow
Prior art date
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Expired - Lifetime
Application number
US05/918,593
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English (en)
Inventor
Charles V. Roberts
William F. Sarra
Peter J. Neuspiel
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RF Delaware Inc
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Roberts Filter Manufacturing Co
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Filing date
Publication date
Application filed by Roberts Filter Manufacturing Co filed Critical Roberts Filter Manufacturing Co
Priority to US05/918,593 priority Critical patent/US4187175A/en
Priority to CA329,770A priority patent/CA1126172A/fr
Priority to AU48226/79A priority patent/AU529053B2/en
Priority to JP7900579A priority patent/JPS5531487A/ja
Application granted granted Critical
Publication of US4187175A publication Critical patent/US4187175A/en
Assigned to RF DELAWARE, INC. reassignment RF DELAWARE, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ROBERTS FILTER MANUFACTURING COMPANY
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Expired - Lifetime legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D24/00—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof
    • B01D24/02—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof with the filter bed stationary during the filtration
    • B01D24/20—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof with the filter bed stationary during the filtration the filtering material being provided in an open container
    • B01D24/22—Downward filtration, the filter material being supported by pervious surfaces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D24/00—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof
    • B01D24/38—Feed or discharge devices
    • B01D24/40—Feed or discharge devices for feeding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D24/00—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof
    • B01D24/46—Regenerating the filtering material in the filter
    • B01D24/4631—Counter-current flushing, e.g. by air
    • B01D24/4642—Counter-current flushing, e.g. by air with valves, e.g. rotating valves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D24/00—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof
    • B01D24/48—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof integrally combined with devices for controlling the filtration
    • B01D24/4861—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof integrally combined with devices for controlling the filtration by flow measuring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D24/00—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof
    • B01D24/48—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof integrally combined with devices for controlling the filtration
    • B01D24/4869—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof integrally combined with devices for controlling the filtration by level measuring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D24/00—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof
    • B01D24/48—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof integrally combined with devices for controlling the filtration
    • B01D24/4884—Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof integrally combined with devices for controlling the filtration by pressure measuring

Definitions

  • This invention relates to a treatment facility of the type that includes a granular media bed to remove suspended solids or other impurities from a liquid mixture, and that employs a backwash operation between treatment operations to restore or otherwise enhance the quality of the bed.
  • This action releases impurities from the bed that were retained during the filter run.
  • the cleaning effect during backwashing is greatly enhanced by causing the media granules to collide on a frequent basis, and this is best achieved by just completely fluidizing the entire portion of bed to be cleaned. It is in this fluidized condition that the individual media granules are, at the same time, closely enough spaced to each other so that a high probability exists for frequent collisions, and far enough apart to release the entrapped impurities.
  • the viscosity of the backwash liquid plays an important role in the backwashing operation. Specifically, it is recognized that the backwash rate or velocity will need to be changed in response to changes in backwash liquid viscosity in order to obtain a desired level of bed expansion, as well as to transport impurities out of the filter chamber. It is also known that the viscosity of a backwash liquid, such as water, will vary with temperature; the viscosity of warm water being lower than that of cold water. Accordingly, to obtain the same desired degree of bed expansion it is necessary to employ a greater backwash rate of flow with warm water than with cold water.
  • the backwash rate established for each stage is determined by a different parameter of the backwashing operation, and although certain steps and controls disclosed in the Babcock U.S. Pat. No. 2,858,024 may be utilized, many features employed in this invention are not remotely suggested by Babcock.
  • the backwash rate employed to enhance the separation of impurities from the granular filter bed is that rate which is just sufficient to fluidize the part of the bed that is to be cleaned, or the entire bed if desired.
  • the rate at which this occurs is generally accompanied by a pronounced change in the differential pressure characteristics across the bed. Specifically, as the backwash rate is gradually increased the differential pressure across the bed also increases until complete fluidization just takes place. At that point the differential pressure remains essentially constant, i.e the change in differential pressure approaches zero. It is at this backwash rate that the bed is just completely fluidized and that the granules forming the bed are optimally spaced to both maximize granuale collisions and release impurities trapped within the bed. This rate will hereinafter sometimes be referred to as the "minimum fluidization rate".
  • the second backwash rate usually will be higher than the first rate, and in the preferred form of this invention is responsive to the temperature of the backwash liquid.
  • a temperature probe is employed to monitor the temperature of the backwash liquid, and the control system suitably adjusts the second backwash rate in accordance with the detected temperature.
  • the second backwash rate is chosen to most effectively remove from the filter the impurities separated from the media in the first stage of the backwash operation. This rate should be chosen to transport the impurities out of the filter as fast as possible without removing the filter bed granules or otherwise damaging the filter bed. This second rate will hereinafter sometimes be referred to as the "transport rate".
  • the most desirable transport rate is generally greater than the minimum fluidization rate, and is not as easily determined as the minimum fluidization rate. In fact, to the best of applicants' knowledge no one has dealt with the problem of determining, or setting the optimum "transport rate" after an initial backwash stage that has been optimized to separate impurities from the filter bed.
  • FIG. 1 is a schematic view of a treatment facility, in the form of a filter, employing a unique backwash control system in accordance with this invention, and
  • FIG. 2 is a schematic fragmentary view showing a modified portion of the FIG. 1 filter.
  • filters employing granular media beds are shown and described herein, together with the unique filter control system for controlling the filtration and backwashing operations thereof.
  • this invention can be employed in other types of treatment facilities in which backwash systems are, or can be employed to clean or otherwise enhance the quality of a granular media bed between treatment operations.
  • a filter 10 is of a conventional type including an inlet conduit 12 for delivering influent to be filtered, and an exit conduit 14 for the filtered effluent.
  • a normally opened pneumatically controlled inlet valve 16 is included in the inlet conduit 12, and remains in its opened position during the filtering run to permit the influent to be directed into the filter.
  • a normally opened pneumatically controlled exit valve 18 is included in the exit conduit 14, and remains in its opened position during the filtering run to permit the filtered effluent to exit the filter.
  • the filter bed 20 is supported on a conventional gravel support bed 22, and this support bed is in turn supported on a false bottom or other suitable support 24.
  • the bottom 24 is a Wheeler bottom, manufactured by Roberts Filter Manufacturing Co., Darby, Pennsylvania 19023.
  • An underdrain chamber 25 is immediately beneath the false bottom 24, and communicates with both the exit conduit 14 and a backwash conduit 26.
  • the backwash conduit 26 includes a pneumatically operated flow control valve 28 that is maintained in a closed position during the filtering operation.
  • the filter 10 is also provided with a waste drain-off conduit 30 for receiving waste during the backwash operation, and a normally closed pneumatically controlled valve 32 associated with this conduit remains in its closed position during the filtering operation.
  • This invention resides in a unique control system for the filter 10, including the method by which the control system functions.
  • the control system of this invention includes a pressure sensing probe, or take-off pipe 40 having an open end positioned in the influent above the unexpanded filter bed 20, but below the drain-off conduit 30, to detect the pressure in this region.
  • a similar pressure probe 42, or takeoff pipe is positioned adjacent the interface between the filter bed 20 and the gravel support 22 to detect the pressure in this region.
  • Both probes 40 and 42 preferably include a screen, or other suitable member (not shown) which is capable of keeping foreign matter out, while permitting liquid to pass through them.
  • a differential pressure unit 44 receives the pressure detected from both probes, compares them, and provides a single pneumatic output 46 indicative of the pressure differential between the probes 40 and 42.
  • the differential pressure unit 44 can be a Model 11 DM Receiver/Transmitter Unit sold by the Foxboro Co. of Foxboro, Ma., and adapted for mid-range zero.
  • the output 46 from the differential pressure unit during the filter run is lower than the output at zero flow (i.e. when the influent is maintained above the filter bed, but prior to the opening of the exit valve 18 in the exit conduit 14).
  • the pressure detecting probe 42 will read at a lower value than the pressure detecting probe 40, and this difference will result in an even lower output 46 than the original output at zero flow.
  • the pressure detected at 42, and hence the pressure differential transmitted at 46 will decrease until a predetermined or preset level is reached to close pneumatic switch 48.
  • the pneumatic switch is adjustable, and is set to close at a preselected pressure differential transmitted by the unit 44.
  • the pressure switch can be a Meletron Model No. 2221, sold by Meletron of Los Angeles, Ca. Closing of the switch 48 can actuate a horn 50, or other suitable signalling device, to indicate to the filter operator that the backwash operation should be manually begun.
  • the operator can manually actuate the pneumatic circuit for the purpose of closing valves 16 and 18, and opening valve 32 to prepare the filter for backwashing.
  • the backwash operation can be started automatically, in which case the closing of the pneumatic switch 48 will energize a backwash sequencer 52 that includes conventional circuit elements arranged to control the backwash operation in the manner described hereinafter. If a horn is also employed to signal the end of a filtering run, the sequencer 52, after being energized for a preset period of time, will open the switch 48 to remove the horn from the circuit. However, the sequencer 52 will remain energized through suitable relays, in a well known manner, to control the backwash operation as will hereinafter be described.
  • the backwash control sequencer 42 When the backwash control sequencer 42 is energized it automatically actuates pneumatic valves 16 and 18 to close off the inlet conduit 12 and the exit conduit 14, respectively, to thereby stop the filter run. Note that this takes place at a preset bed loss indicative of the need to clean the filter bed 20.
  • the sequencer 52 actuates the pneumatic valve 32 to open the waste drain-off conduit 30, and also actuates the pneumatic flow controller 54.
  • the flow controller is of the type having a remote set, such as Foxboro Model No. 130F, and upon being actuated, it opens the pneumatic valve 28 in the backwash conduit 26 to a preset position for obtaining an initial preset flow to begin the backwash operation.
  • This flow is set to be lower than the desired fludization rate to permit commencement of reverse flow through the bed 20 without damaging it.
  • This initial rate is detected by the controller 54 through a hydraulic flow rate measuring unit 55 included in the backwash conduit 26.
  • the flow rate measuring unit 55 can include a Foxboro 11 DM Transmitter 55a combined with a F & P 10F1070 Tube 55b.
  • a fluidization ramping device 56 is actuated to gradually increase the pneumatic pressure through the flow controller 54, and thereby gradually increase the opening of the pneumatic valve 28 to gradually increase the backwash flow rate.
  • the backwash differential pressure output from the differential pressure transmitting unit 44 likewise increases. This increase in the output results from the pressure at probe 42 being greater then the pressure at the probe 40 and the increase continues at an essentially constant rate as the bed begins to expand.
  • the differential pressure becomes constant and the change in differential pressure abruptly becomes essentially zero. In other words, when the bed just becomes completely fluidized the pressure drop across it reaches a constant value.
  • the output 46 from the differential pressure unit 44 also remains constant, and thereby closes differential pressure switch 58 to stop and lock in the ramping device 56 so that the backwash rate will not be further increased.
  • the backwash rate is maintained at the level required to just fluidize the bed, i.e. the "minimum fluidization rate".
  • the differential pressure switch 58 can be of various types; one representative type being Meletron Model No. 2262. Since the switch 58 is closed when it receives a constant input signal indicative of a zero change in differential pressure, it is kept out of the control circuit until the ramping device 56 is actuated to cause a change in differential pressure to take place. When the ramping device 56 is actuated to gradually increase the backwash rate through the filter 10, it also completes the circuit to the differential pressure switch 58 to permit it to operate as described above. If the switch 58 were in the circuit prior to actuation of the ramping device 56 it would receive a constant input signal 46 from the differential pressure unit 44, and would be closed to prevent the operation of the ramping device.
  • the backwash rate through the filter bed is constant; thereby providing a constant differential pressure or head loss across the filter bed 20.
  • the backwash rate through the filter will gradually increase, thereby gradually changing the pressure drop across the filter bed to provide a variable output 46 until such time as complete fluidization is achieved. At that time, as described above, the output 46 will be constant to actuate the switch 58 and lock in the ramping device 56 at the proper operating condition to maintain the minimum fluidization backwash rate.
  • Closing of the switch 58 not only locks in the ramping device 56, but also counts down one unit toward zero on a preset counter 60, and actuates a preset fluidization timer 62.
  • the preset counter 60 can be of any conventional type, such as an ATC Model No. 326, manufactured by Automatic Timing & Controls Co. in King of Prussia, Pa., and the setting on the counter 60 determines the number of times that the backwash cycle will be repeated prior to returning to a filtration run, as will be explained in greater detail later in this application.
  • the timer 62 can also be of any conventional type, such as ATC Model No. 325, and controls the length of time at which the backwash rate is maintained at the minimum fluidization level.
  • the timer 62 After the timer 62 times out it automatically starts the transport stage of the backwash operation. In this stage the backwash flow rate is adjusted to a level that is most efficient, or desired, for removing from the filter 10 those particular impurities separated from the filter bed 20 during the previous fluidization stage. This rate, in virtually all cases, will be higher than the minimum fluidization rate.
  • timer 64 automatically actuates timer 64, which in turn actuates a programmable transport stage rate controller 66, such as Foxboro Model No. 135ZG, for the length of time set on timer 64.
  • the time that is set on timer 64 is the length of time that the transport stage is active.
  • the controller 66 upon being actuated, will receive an input signal from a temperature sensor 68 employed to sense the temperature of the backwash liquid, and in response to the input signal, will compute the appropriate signal to be sent to the flow controller 54 to adjust the control valve 28 for establishing the desired transport rate or velocity, as detected by the flow rate measuring unit 55.
  • the rate controller 66 is programmed to change the backwash flow rate based on changes in the temperature of the backwash water; a parameter that is indicative of viscosity. Applicants have found that changes in viscosity of the backwash water, due to change in temperature, should be taken into account in establishing the desired transport rate for removing fluidized particulate impurities from the filter 10, after those impurities have been separated from the filter bed 20 in the previous fluidization stage of the backwash operation. For example, if temperature of the backwash water decreases, its viscosity will increase, and if the transport velocity or rate is maintained at the same level, it can, because of the higher viscosity of the backwash water, actually wash out media granules. Therefore, when the temperature of the backwash water decreases the transport rate is decreased, and when the temperature of the backwash water increases the transport rate is increased.
  • the desired relationship between backwash rate and the backwash liquid temperature can be determined empirically for different filters by employing trial backwash runs at different backwash temperatures. This relationship can then be programmed into the transport stage rate controller 66 to provide the desired automatic control of the backwash rate during the transport stage of the backwash operation.
  • the backwash sequencer 52 will actuate the flow controller 54 to close the pneumatic valve 28 in the backwash conduit 26, and thereby stop the flow of backwash water into the filter 10.
  • the sequencer 52 will also be actuated to permit the control valve 32 in the drain-off conduit 30 to move to its normally closed position, and to permit the inlet and exit valves 16 and 18 in the inlet conduit 12 and exit conduit 14 to move to their normally opened position. This prepares the filter 10 for its filtering mode of operation.
  • the backwash sequencer 52 will be operated to actuate the flow controller 54 to establish a setting for pneumatic valve 28, for a preset time, that provides an initial backwash flow rate lower than the fluidization rate. Thereafter, the sequencer 52 will energize the ramping device 56, and the sequence of operations through the fluidization rate stage and the transport rate stage will be repeated. The sequence will continue to be repeated until counter 60 ultimately reaches zero, at which time a filter run will be commenced.
  • the counter 60 is employed to set the number of times that the backwash operation will sequencially pass through the minimum fluidization rate and the transport rate prior to returning to the next filtering run.
  • This arrangement provides a great deal of flexibility in backwashing the filter. For example, if the influent being treated is heavily contaminated, resulting in the entrapment of a large quantity of impurities in the filter bed 20 during the filter run, it may be most desirable and efficient to sequence through the minimum fluidization rate and the transport rate several times in a backwash cycle, rather than attempting to separate all of the impurities out of the bed in a single fluidization stage, and then attempting to remove all of the separated impurities from the filter chamber in a single transport stage.
  • a modified filter 10a is shown with portions of its control circuitry that differ from the circuitry shown in FIG. 1.
  • the filter 10a is a multi-media unit including two different types of media, 20a and 20b, respectively.
  • the upper media 20a can be anthracite
  • the lower media 20b can be sand.
  • the specific types or quantities of different media employed in the filter is not considered to be a limitation on the present invention.
  • control system shown in FIG. 1 can be employed by positioning the pressure detecting probe 40 above the top of the media 20a, substantially in the same location that it occupies in the FIG. 1 embodiment, and by positioning the lower pressure detecting probe 42 at the interface between the gravel bed and the lower media layer 20b.
  • the filter bed may be desirable to form the filter bed with an upper media layer 20a that will become fluidized at a different backwash rate than the media layer 20b.
  • the upper layer 20a may require more frequent scouring, and therefore more frequent fluidization than the lower layer.
  • the media employed to form the upper layer will be chosen to permit the upper layer to expand at a lower backwash flow rate than the lower layer. Then, for example, the backwash operation may be carried out to establish minimum fluidization rate conditions for the upper layer 20a during every backwash cycle, and on a less frequent basis for the lower layer 20b.
  • a first pressure probe 41a is placed adjacent the interface between the media 20a and the media 20b, and a second pressure probe 42a is placed adjacent the interface of the lower media 20b and the gravel layer 22a.
  • These two pressure probes through a single connection, are joined to a differential pressure unit 44a, which can be identical to the differential pressure unit 44 (FIG. 1).
  • the probes 41a and 42a are individually valved at 41a' and 42a', respectively, to communicate the desired probe with the unit 44a.
  • a reference probe 40a is positioned above the upper media layer 20a, and is also in communication with the differential pressure unit 44a.
  • the reference probe 40a will either coact with the probe 41a or the probe 42a to monitor the pressure drop across the media layer 20a or 20b, respectively.
  • the control system will operate in the same manner as described above in connection with FIG. 1 by monitoring the headloss across the desired layer(s) of the filter bed to be expanded, and locking in a backwash rate which just completely fluidizes those layer(s).
  • an automatic control circuit is included in the programmed sequencer (not shown) to automatically open and/or close the solenoid valves 41a' and 42a' associated with the respective pressure probes 41a and 42a in a desired sequence to thereby control the backwash operation as desired.
  • a filter run can be terminated automatically by programming the controls to activate the backwash sequencer at a predetermined headloss through the entire filter bed, or only part of it, as determined, or detected by pressure probes that are communicated with the differential pressure unit 44a.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Filtration Of Liquid (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US05/918,593 1978-06-23 1978-06-23 Treatment facility with backwash control system Expired - Lifetime US4187175A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US05/918,593 US4187175A (en) 1978-06-23 1978-06-23 Treatment facility with backwash control system
CA329,770A CA1126172A (fr) 1978-06-23 1979-06-14 Installation de traitement a systeme de controle du lavage a contre-courant
AU48226/79A AU529053B2 (en) 1978-06-23 1979-06-20 Backwash control for gravity filter
JP7900579A JPS5531487A (en) 1978-06-23 1979-06-22 Backwash device of water disposal plant and its method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US05/918,593 US4187175A (en) 1978-06-23 1978-06-23 Treatment facility with backwash control system

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US4187175A true US4187175A (en) 1980-02-05

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US05/918,593 Expired - Lifetime US4187175A (en) 1978-06-23 1978-06-23 Treatment facility with backwash control system

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US (1) US4187175A (fr)
JP (1) JPS5531487A (fr)
AU (1) AU529053B2 (fr)
CA (1) CA1126172A (fr)

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US4439325A (en) * 1982-08-06 1984-03-27 Cpc Engineering Corporation Pressurized filtration system
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WO1999024140A1 (fr) * 1997-11-07 1999-05-20 The Roberts Filter Group Systeme utilisant la pression differentielle pour surveiller un lit filtrant
US5975111A (en) * 1997-09-29 1999-11-02 The Boeing Company Waste tank clog removal system
US6342163B1 (en) 1999-11-12 2002-01-29 United States Filter Corporation Apparatus and method for sanitizing and cleaning a filter system
US20040020870A1 (en) * 2002-07-31 2004-02-05 Amburgey James Emanuel Method of filter backwashing: extended terminal subfluidization wash
US20040129653A1 (en) * 2000-11-03 2004-07-08 Frederick Spruce Water treatment system
US20050109706A1 (en) * 1999-04-30 2005-05-26 David Hambley Filter underdrain system for backwash flow and method for measuring same
US20050184011A1 (en) * 2004-02-20 2005-08-25 Fields William M. Car wash water reclamation system
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US20070175832A1 (en) * 2006-01-27 2007-08-02 Roberts R L Method and apparatus for monitoring an underdrain of a filter system
KR100774881B1 (ko) 2006-06-14 2007-11-08 한국건설기술연구원 수온에 따른 모래여과공정의 역세척수 유속제어 장치 및방법
US20080251466A1 (en) * 2005-02-17 2008-10-16 Conserv Manufacturing Waste Water Recovery System
US20100176071A1 (en) * 2008-06-19 2010-07-15 Nagaoka International Corporation Water treatment apparatus and a method for cleaning a filter layer of a water treatment apparatus
KR101152875B1 (ko) 2011-11-25 2012-06-12 주식회사 부강테크 3지점 압력측정을 통한 수처리시설의 운영제어방법 및 이를 활용한 운영제어장치
US20140190907A1 (en) * 2011-07-25 2014-07-10 Nagaoka International Corporation Upper-layer cleaning device for water treatment device, and method for cleaning water treatment device filter layer
EP2859928A1 (fr) * 2013-10-08 2015-04-15 Gidelmar, S.A. Procédé de rétrolavage de filtre
US20150314220A1 (en) * 2012-12-04 2015-11-05 Enhydra Ltd. Filtration arrangement and method
US20160114265A1 (en) * 2012-02-12 2016-04-28 Ide Technologies Ltd. Integrated unit for intake and pretreatment with local backwashing
US20200326219A1 (en) * 2019-04-12 2020-10-15 Norman C. Whitehead Drop Test Measuring System and Method(s) of Use Thereof
US11247918B2 (en) * 2017-12-08 2022-02-15 Westech Engineering, Llc Multi-media clarification systems and methods
CN119596790A (zh) * 2024-12-02 2025-03-11 天津水科机电有限公司 一种基于反冲洗滤水器的远程参数自调控方法
CN119874137A (zh) * 2025-03-27 2025-04-25 深圳市深水龙岗水务集团有限公司 一种基于半絮凝的叠合式高效净水方法

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EP0150919A3 (fr) * 1984-01-12 1986-06-04 Water Research Centre Dispositif et procédé de contrôle du rinçage à contre-courant d'un filtre
US4608158A (en) * 1984-08-01 1986-08-26 Web Italia S.R.L. Feeding installation for the dampening solution in offset printing processes
US4929363A (en) * 1987-02-27 1990-05-29 Filtration L.T.D. Method for filtering a fluid
US5019276A (en) * 1987-10-07 1991-05-28 Bk Va-Leveranser Ab Method of and plant for purifying water
US5137644A (en) * 1991-05-14 1992-08-11 James M. Montgomery Consulting Engineers, Inc. Pipe connection system for multiple water treatment filters
US5484536A (en) * 1991-09-17 1996-01-16 Kabushiki Kaisha Toshiba Filter backwash control method and apparatus
US20070115472A1 (en) * 1997-01-02 2007-05-24 Jung Wayne D Apparatus and method for measuring optical characteristics of an object
NL1005789C2 (nl) * 1997-04-10 1998-10-14 Remon B V Inrichting en werkwijze voor het filteren van water.
EP0878225A1 (fr) * 1997-04-10 1998-11-18 Remon B.V. Dispositif et procédé de filtrage d'eau
US5975111A (en) * 1997-09-29 1999-11-02 The Boeing Company Waste tank clog removal system
WO1999024140A1 (fr) * 1997-11-07 1999-05-20 The Roberts Filter Group Systeme utilisant la pression differentielle pour surveiller un lit filtrant
US5980755A (en) * 1997-11-07 1999-11-09 Rg, Delaware, Inc. Methods and apparatus for monitoring a filter bed by differential pressure
US6159384A (en) * 1997-11-07 2000-12-12 Rg, Delaware, Inc. Methods and apparatus for monitoring a filter bed by differential pressure
US20050109706A1 (en) * 1999-04-30 2005-05-26 David Hambley Filter underdrain system for backwash flow and method for measuring same
US7326351B2 (en) * 1999-04-30 2008-02-05 David Hambley Filter underdrain system for backwash flow and method for measuring same
US6419823B2 (en) 1999-11-12 2002-07-16 United States Filter Corporation Apparatus and method for sanitizing and cleaning a filter system
US6342163B1 (en) 1999-11-12 2002-01-29 United States Filter Corporation Apparatus and method for sanitizing and cleaning a filter system
US20040129653A1 (en) * 2000-11-03 2004-07-08 Frederick Spruce Water treatment system
US7029578B2 (en) * 2000-11-03 2006-04-18 Spruce International Separations Water treatment system
US20040020870A1 (en) * 2002-07-31 2004-02-05 Amburgey James Emanuel Method of filter backwashing: extended terminal subfluidization wash
US20050184011A1 (en) * 2004-02-20 2005-08-25 Fields William M. Car wash water reclamation system
US20080251466A1 (en) * 2005-02-17 2008-10-16 Conserv Manufacturing Waste Water Recovery System
US20100282651A1 (en) * 2006-01-27 2010-11-11 Roberts R Lee Method and apparatus for monitoring an underdrain of a filter system
US7754089B2 (en) 2006-01-27 2010-07-13 Rg Delaware, Inc. Method and apparatus for monitoring an underdrain of a filter system
US20070175832A1 (en) * 2006-01-27 2007-08-02 Roberts R L Method and apparatus for monitoring an underdrain of a filter system
US7921697B2 (en) 2006-01-27 2011-04-12 Rg Delaware, Inc. Method and apparatus for monitoring an underdrain of a filter system
KR100774881B1 (ko) 2006-06-14 2007-11-08 한국건설기술연구원 수온에 따른 모래여과공정의 역세척수 유속제어 장치 및방법
US20100176071A1 (en) * 2008-06-19 2010-07-15 Nagaoka International Corporation Water treatment apparatus and a method for cleaning a filter layer of a water treatment apparatus
US8110116B2 (en) * 2008-06-19 2012-02-07 Nagaoka International Corporation Water treatment apparatus and a method for cleaning a filter layer of a water treatment apparatus
US20140190907A1 (en) * 2011-07-25 2014-07-10 Nagaoka International Corporation Upper-layer cleaning device for water treatment device, and method for cleaning water treatment device filter layer
US9573082B2 (en) * 2011-07-25 2017-02-21 Nagaoka International Corporation Upper-layer cleaning device for water treatment device, and method for cleaning water treatment device filter layer
KR101152875B1 (ko) 2011-11-25 2012-06-12 주식회사 부강테크 3지점 압력측정을 통한 수처리시설의 운영제어방법 및 이를 활용한 운영제어장치
US10926201B2 (en) * 2012-02-12 2021-02-23 Ide Technologies Ltd. Integrated unit for intake and pretreatment with local backwashing
US20160114265A1 (en) * 2012-02-12 2016-04-28 Ide Technologies Ltd. Integrated unit for intake and pretreatment with local backwashing
US20150314220A1 (en) * 2012-12-04 2015-11-05 Enhydra Ltd. Filtration arrangement and method
EP2859928A1 (fr) * 2013-10-08 2015-04-15 Gidelmar, S.A. Procédé de rétrolavage de filtre
US11247918B2 (en) * 2017-12-08 2022-02-15 Westech Engineering, Llc Multi-media clarification systems and methods
US20200326219A1 (en) * 2019-04-12 2020-10-15 Norman C. Whitehead Drop Test Measuring System and Method(s) of Use Thereof
US11713991B2 (en) * 2019-04-12 2023-08-01 Norman C. Whitehead Drop test measuring system and method(s) of use thereof
CN119596790A (zh) * 2024-12-02 2025-03-11 天津水科机电有限公司 一种基于反冲洗滤水器的远程参数自调控方法
CN119874137A (zh) * 2025-03-27 2025-04-25 深圳市深水龙岗水务集团有限公司 一种基于半絮凝的叠合式高效净水方法

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AU529053B2 (en) 1983-05-26
CA1126172A (fr) 1982-06-22
AU4822679A (en) 1980-03-06

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